Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
  • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
  • C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
  • B01D15/08—Selective adsorption, e.g. chromatography
  • B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
  • B01D15/20—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to the conditioning of the sorbent material
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
  • B01D15/08—Selective adsorption, e.g. chromatography
  • B01D15/26—Selective adsorption, e.g. chromatography characterised by the separation mechanism
  • B01D15/36—Selective adsorption, e.g. chromatography characterised by the separation mechanism involving ionic interaction, e.g. ion-exchange, ion-pair, ion-suppression or ion-exclusion
  • B01D15/361—Ion-exchange
  • B01D15/362—Cation-exchange
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J39/00—Cation exchange; Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
  • B01J39/04—Processes using organic exchangers
  • B01J39/05—Processes using organic exchangers in the strongly acidic form
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J39/00—Cation exchange; Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
  • B01J39/08—Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
  • B01J39/16—Organic material
  • B01J39/18—Macromolecular compounds
  • B01J39/20—Macromolecular compounds obtained by reactions only involving unsaturated carbon-to-carbon bonds
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J47/00—Ion-exchange processes in general; Apparatus therefor
  • B01J47/014—Ion-exchange processes in general; Apparatus therefor in which the adsorbent properties of the ion-exchanger are involved, e.g. recovery of proteins or other high-molecular compounds
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J47/00—Ion-exchange processes in general; Apparatus therefor
  • B01J47/016—Modification or after-treatment of ion-exchangers
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
  • C07C41/01—Preparation of ethers
  • C07C41/34—Separation; Purification; Stabilisation; Use of additives
  • C07C41/36—Separation; Purification; Stabilisation; Use of additives by solid-liquid treatment; by chemisorption
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
  • B01D15/08—Selective adsorption, e.g. chromatography
  • B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
  • B01D15/18—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns
  • B01D15/1807—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns using counter-currents, e.g. fluidised beds

Definitions

• the present invention generally relates to systems and methods for reducing aldehyde levels in diethylene glycol and/or triethylene glycol. More specifically, the present invention relates to systems and methods for reducing aldehyde levels in diethylene glycol and/or triethylene glycol using monoethylene glycol soaked ion-exchange resins.
• Ethylene glycols including monoethylene glycol, diethylene glycol, triethylene glycol, and polyethylene glycol, are a group of versatile chemicals used in many areas of the chemical industry.
• monoethylene glycol (MEG) is used as an antifreeze and coolant for engines and an intermediate for producing polyester fibers and polyethylene terephthalate (PET), which is used for producing plastic bottles.
• Diethylene glycol (DEG) can be used to produce polyurethanes, plasticizers, and organic solvents.
• Triethylene glycol (TEG) is often used as a plasticizer and moisture-retaining agent.
• Polyethylene glycol (PEG) is used in perfumes, cosmetics, lubricants, and plasticizers.
• ethylene glycols especially diethylene glycol and triethylene glycol, contain aldehyde as a contaminant due to various factors including oxidation of the ethylene glycols.
• Aldehyde can also be introduced into ethylene glycols from a reactor used for producing ethylene oxide, which is a reactant for producing ethylene glycols.
• One of methods commonly used to reduce the aldehyde content in ethylene glycols includes treating the ethylene glycol with a strong acidic cation exchange resin. In this method, the ion-exchange resin is first soaked in the target product (i.e., the ethylene glycol) for several hours for the resin to undergo swelling.
• the target product is then flowed through the soaked ion-exchange resin to remove the aldehyde.
• this method has been proven to be only highly effective for removing aldehyde content in monoethylene glycol.
• the performance of the strong acidic cation exchange resin in treating diethylene glycol and triethylene glycol is relatively poor.
• a solution to at least some of the above-mentioned problems associated with the reduction of aldehyde content in a mixture comprising diethylene glycol and/or triethylene glycol has been discovered.
• the solution resides in a method of lowering aldehyde content in diethylene glycol and/or triethylene glycol using monoethylene glycol soaked ion-exchange resin.
• This method avoids using diethylene glycol and/or triethylene glycol to soak the ion-exchange resin before treating the diethylene glycol and/or triethylene glycol. This can be beneficial for at least preventing reduction of efficiency of the ion- exchange resin caused by soaking in diethylene glycol and/or triethylene glycol.
• this method is capable of maintaining high efficiency of the ion-exchange resin for removing aldehyde. Therefore, the method of the present invention provides a technical solution to at least some of the problems associated with the conventional methods for reducing aldehyde content in ethylene glycols.
• Embodiments of the invention include a method of lowering aldehyde content of a mixture comprising diethylene glycol (DEG) and 5 to 200 ppm aldehyde.
• the method comprises soaking ion-exchange resin in monoethylene glycol.
• the method further comprises contacting the soaked ion-exchange resin with the mixture to produce a product comprising DEG and less than 15 ppm aldehyde.
• Embodiments of the invention include a method of lowering aldehyde content of a mixture comprising diethylene glycol (DEG) and 5 to 200 ppm aldehyde.
• the method comprises soaking ion-exchange resin in monoethylene glycol for at least 4 hours at a temperature of 0 to 60 °C.
• the method further comprises contacting the soaked ion-exchange resin with the mixture to produce a product comprising DEG and less than 15 ppm aldehyde.
• Embodiments of the invention include a method of lowering aldehyde content of a mixture comprising triethylene glycol (TEG) and 5 to 200 ppm aldehyde.
• the method comprises soaking ion-exchange resin in monoethylene glycol.
• the method further comprises contacting the soaked ion-exchange resin with the mixture to produce a product comprising TEG and less than 15 ppm aldehyde.
• Embodiments of the invention include a method of lowering aldehyde content of a mixture comprising triethylene glycol (TEG) and 5 to 200 ppm aldehyde.
• the method comprises soaking ion-exchange resin in monoethylene glycol for at least 4 hours at a temperature of 0 to 60 °C.
• the method further comprises contacting the soaked ion-exchange resin with the mixture to produce TEG comprising less than 15 ppm aldehyde.
• wt. % refers to a weight, volume, or molar percentage of a component, respectively, based on the total weight, the total volume, or the total moles of material that includes the component.
• 10 moles of component in 100 moles of the material is 10 mol. % of component.
• primarily means greater than any of 50 wt. %, 50 mol. %, and 50 vol. %.
• “primarily” may include 50.1 wt. % to 100 wt. % and all values and ranges there between, 50.1 mol. % to 100 mol. % and all values and ranges there between, or 50.1 vol. % to 100 vol. % and all values and ranges there between.
• FIG. 1 shows a schematic diagram for a system of reducing aldehyde content in a mixture comprising aldehyde and diethylene glycol and/or triethylene glycol, according to embodiments of the invention.
• FIG. 2 shows a schematic flowchart for a method of reducing aldehyde content in a mixture comprising aldehyde and diethylene glycol and/or triethylene glycol, according to embodiments of the invention.
• the solution is premised on a method of lowering aldehyde content in diethylene glycol and/or triethlyene glycol by contacting the aldehyde containing diethylene glycol and/or triethlyene glycol with an ion- exchange resin that is soaked in monoethylene glycol.
• this method is capable of retaining the aldehyde removing/reducing/lowering ability for the ion-exchange resin before the diethylene glycol and/or triethylene glycol is treated for aldehyde removal, resulting in high aldehyde lowering efficiency.
• the system for lowering aldehyde in DEG and/or TEG can include a bed of an ion-exchange resin, and a shell for containing the bed.
• a schematic diagram is shown of system 100 for reducing aldehyde content in DEG and/or TEG.
• system 100 includes bed 101 of an ion-exchange resin.
• the ion-exchange resin is configured to remove aldehyde from diethylene glycol and/or triethylene glycol.
• the ion-exchange resin includes crosslinked polystyrene, polystyrene crosslinked with divinylbenzene, or combinations thereof.
• the ion-exchange resin is an acid resin, preferably a strong acid resin including resins with sulfonic acid functional groups.
• the ion exchange resin may include strong acidic cation exchange resin.
• Non-limiting examples of the strong acidic cation exchange resin include sodium polystyrene sulfonate, poly(2-acrylamido-2-methyl-l-propanesulfonic acid), or combinations thereof.
• bed 101 comprises the ion- exchange resin in the form of beads.
• the beads of bed 101 have an average size of 0.3 to 1.5 mm and all ranges and values there between including ranges of 0.3 to 0.6 mm, 0.6 to 0.9 mm, 0.9 to 1.2 mm, and 1.2 to 1.5 mm.
• the beads of bed 101 may be macroporous with an average pore size greater than 50 A.
• bed 101 may be disposed in shell 102.
• shell 102 may include a column.
• Shell 102 may be made of a material comprising stainless steel.
• the column has a length to diameter ratio in a range of 0.5 to 5 and all ranges and values there between including ranges of 0.5 to 1.0, 1.0 to 1.5, 1.5 to 2.0, 2.0 to 2.5, 2.5 to 3.0, 3.0 to 3.5, 3.5 to 4.0, 4.0 to 4.5, and 4.5 to 5.0.
• bed 101 occupies about 50 to 80% of the volume of shell 102 and all ranges and values there between.
• system 100 includes inlet 103 disposed on an end of shell 102, configured to receive feed stream 11 into shell 102.
• inlet 103 is further configured to load resin into shell 102.
• system 100 may include a separate resin loading inlet configured to receive resin in shell 102.
• inlet 103 may be further configured to receive soaking medium stream 12 into shell 102. Soaking medium stream 12 may include monoethylene glycol.
• soaking medium stream 12 includes less than 10 ppm aldehyde.
• inlet 103 may be further still configured to receive inert gas stream 13 into shell 102. Inert gas stream may include nitrogen.
• system 100 may include soaking medium inlet 104 disposed on shell 102, configured to receive soaking medium stream 12 into shell 102.
• system 100 may include gas inlet 105 disposed on shell 102, configured to receive inert gas stream 13 into shell 102.
• system 100 includes outlet 106 disposed on the end of shell 102 that is opposite to inlet 103.
• outlet 106 may be configured to release one or more of product stream 14, exiting gas stream 15, and spent soaking medium stream 16 from shell 102.
• system 100 may include outlet 106, gas outlet 107, and soaking medium outlet 108 configured to release product stream 14, exiting gas stream 15, and spent soaking medium stream 16 from shell 102, respectively.
• system 100 may include resin trap 109 disposed downstream to bed 101. Resin trap 109 may be configured to substantially prevent ion-exchange resin from inadvertently exiting shell 102. In certain embodiments of the invention, resin trap 109 can be disposed inside or outside of shell 102. According to certain embodiments of the invention, system 100 may further include resin inlet 110 and resin outlet 111 configured to receive the ion-exchange resin into shell 102 and release the ion-exchange resin from shell 102, respectively.
• Methods of lowering aldehyde content in diethylene glycol and/or triethylene glycol using ion-exchange resin have been discovered. Certain embodiments of the method are capable of improving the efficiency of ion-exchange resin for reducing aldehyde content in DEG and/or TEG compared to conventional methods. As shown in FIG. 2, certain embodiments of the invention include method 200 for lowering aldehyde content in a mixture comprising (i) diethylene glycol and/or triethylene glycol and (ii) aldehyde. Method 200 may be implemented by system 100, as shown in FIG. 1.
• method 200 includes soaking ion-exchange resin in monoethylene glycol.
• the ion-exchange resin is packed as bed 101.
• the monoethylene glycol contains 0 to 10 ppm of aldehyde and all ranges and values there between including ranges of 0 to 0.5 ppm, 0.5 to 1.0 ppm, 1.0 to 1.5 ppm, 1.5 to 2.0 ppm, 2.0 to 2.5 ppm, 2.5 to 3.0 ppm, 3.0 to 3.5 ppm, 3.5 to 4.0 ppm, 4.0 to 4.5 ppm, 4.5 to 5.0 ppm, 5.0 to 5.5 ppm, 5.5 to 6.0 ppm, 6.0 to 6.5 ppm, 6.5 to 7.0 ppm, 7.0 to 7.5 ppm, 7.5 to 8.0 ppm, 8.0 to 8.5 ppm, 8.5 to 9.0 ppm,
• the ion- exchange resin is soaked for at least 4 hours, preferably more than 6 hours.
• ion-exchange resin may have contained up to 60 wt.% water.
• ion-exchange resin is capable of expanding to a volume that is 1 to 3 times of the volume before the ion-exchange resin is soaked.
• the soaking at block 201 is carried out at a temperature of 0 to 60 °C and all ranges and values there between including ranges of 0 to 3 °C, 3 to 6 °C, 6 to 9 °C, 9 to 12 °C, 12 to 15 °C, 15 to 18 °C, 18 to 21 °C, 21 to 24 °C, 24 to 27 °C, 27 to 30 °C, 30 to 33 °C, 33 to 36 °C, 36 to 39 °C, 39 to 42 °C, 42 to 45 °C, 45 to 48 °C, 48 to 51 °C, 51 to 54 °C, 54 to 57 °C, and 57 to 60 °C.
• bed 101 is further flushed with monoethylene glycol.
• method 200 includes bubbling an inert gas through bed 101 of the ion exchange resin.
• the bubbling at block 202 is configured to remove fine particles from the ion exchange resin of bed 101. Bubbling at block 202 may be further configured to ensure proper packing, which entails sufficient contact between resin and the fluid such that the fluid does not bypass part of the resin bed of bed 101.
• the inert gas includes nitrogen.
• the inert gas is bubbled through bed 101 at a flowrate such that a light fluidization of resin is developed.
• the bubbling at block 202 may be carried out at a temperature of 0 to 60 °C and all ranges and values there between including ranges of 0 to 3 °C, 3 to 6 °C, 6 to 9 °C, 9 to 12 °C, 12 to 15 °C, 15 to 18 °C, 18 to 21 °C, 21 to 24 °C, 24 to 27 °C, 27 to 30 °C, 30 to 33 °C, 33 to 36 °C, 36 to 39 °C, 39 to 42 °C, 42 to 45 °C, 45 to 48 °C, 48 to 51 °C, 51 to 54 °C, 54 to 57 °C, and 57 to 60 °C.
• method 200 includes contacting the soaked ion exchange resin with the mixture to produce a product comprising (i) diethylene or triethylene glycol and (ii) aldehyde with a concentration lower than the aldehyde concentration in the mixture.
• the mixture comprises 5 to 200 ppm aldehyde and all ranges and values there between including 5 to 10 ppm, 10 to 20 ppm, 20 to 30 ppm, 30 to 40 ppm, 40 to 50 ppm, 50 to 60 ppm, 60 to 70 ppm, 70 to 80 ppm, 80 to 90 ppm, 90 to 100 ppm, 100 to 110 ppm, 110 to 120 ppm, 120 to 130 ppm, 130 to 140 ppm, 140 to 150 ppm, 150 to 160 ppm, 160 to 170 ppm, 170 to 180 ppm, 180 to 190 ppm, and 190 to 200 ppm.
• the product comprises 0 to 15 ppm aldehyde and all ranges and values there between including ranges of 0 to 1 ppm, 1 to 2 ppm, 2 to 3 ppm, 3 to 4 ppm, 4 to 5 ppm, 5 to 6 ppm, 6 to 7 ppm, 7 to 8 ppm, 8 to 9 ppm, 9 to 10 ppm, 10 to 11 ppm, 11 to 12 ppm, 12 to 13 ppm , 13 to 14 ppm, and 14 to 15 ppm.
• the contacting is carried out at a temperature of 0 to 65 °C and all ranges and values there between including ranges of 0 to 3 °C, 3 to 6 °C, 6 to 9 °C, 9 to 12 °C, 12 to 15 °C, 15 to 18 °C, 18 to 21 °C, 21 to 24 °C, 24 to 27 °C, 27 to 30 °C, 30 to 33 °C, 33 to 36 °C, 36 to 39 °C, 39 to 42 °C, 42 to 45 °C, 45 to 48 °C, 48 to 51 °C, 51 to 54 °C, 54 to 57 °C, 57 to 60 °C, 60 to 63 °C, and 63 to 65 °C.
• the contacting at block 203 including flowing the DEG and/or TEG through bed 101 of ion-exchange resin.
• the DEG and/or TEG is flowed through the ion-exchanger resin at a flow rate of 0.1 to 10 bed volumes per hour (a liquid hourly space velocity of 0.1 to 10 hr 1 ) and all ranges and values there between including 0.1 to 0.2 hr 1 , 0.2 to 0.3 hr 1 , 0.3 to 0.4 hr 1 , 0.4 to 0.5 hr 1 , 0.5 to 0.6 hr 1 , 0.6 to 0.7 hr 1 , 0.7 to 0.8 hr 1 , 0.8 to 0.9 hr 1 , 0.9 to 1 hr 1 , 1 to 2 hr 1 , 2 to 3 hr 1 , 3 to 4 hr 1 , 4 to 5 hr 1 , 5 to 6 hr 1
• method 200 may further include back- flushing the product produced at block 203 in a direction opposite to the DEG and/or TEG flow direction at block 203.
• Back-flushing may be further conducted during start-up of method 200, after soaking step at block 201 when contacting with the product is started. Back-flushing may further be performed periodically (e.g., every 2-4 months) during the whole process of method 200.
• the back flushing may be configured to further remove empty pockets in bed 101. In certain embodiments of the invention, the back flushing is carried out for less than 2 hours.
• method 200 is a continuous process.
• Embodiment l is a method of lowering aldehyde content of a mixture containing (i) a plural ethylene glycol, wherein the plural ethylene glycol is diethylene glycol (DEG) or triethylene glycol (TEG), and (ii) 5 to 200 ppm aldehyde.
• the method includes soaking ion- exchange resin in monoethylene glycol.
• the method further includes contacting the soaked ion-exchange resin with the mixture containing the plural ethylene glycol and 5 to 200 ppm aldehyde to produce a product containing the plural ethylene glycol and less than 15 ppm aldehyde.
• Embodiment 2 is the method of embodiment 1, wherein the ion-exchange resin is soaked in monoethylene glycol for at least 4 hours.
• Embodiment 3 is the method of either of embodiments 1 or 2, wherein the ion-exchange resin is soaked in monoethylene glycol at a temperature of 0 to 60 °C.
• Embodiment 4 is the method of any of embodiments 1 to 3, wherein the ion-exchange resin is acidic.
• Embodiment 5 is the method of any of embodiments 1 to 4, wherein the product contains 10 ppm or less aldehyde.
• Embodiment 6 is the method of any of embodiments 1 to 5, wherein the ion-exchange resin is packed in a bed.
• Embodiment 7 is the method of embodiment 6, wherein in the contacting step, the mixture is flowed through the ion-exchanger resin at a flow rate of 0.1 to 10 bed volumes per hour.
• Embodiment 8 is the method of either of embodiments 6 or 7, further including, prior to the contacting step, bubbling an inert gas through the bed of ion-exchange resin, and back-flushing the bed with the product.
• Embodiment 9 is the method of embodiment 8, wherein the steps of bubbling the inert gas and back-flushing are adapted to remove fine particles from the bed and/or ensure proper packing of the bed.
• Embodiment 10 is the method of either of embodiments 8 or 9, wherein the inert gas includes nitrogen.
• Embodiment 11 is the method of any of embodiments 8 to 10, wherein the back-flushing is carried out for less than 2 hours.
• Embodiment 12 is the method of any of embodiments 8 to 11, further including, prior to the back-flushing step, flushing the bed of ion- exchange resin with monoethylene glycol.
• Embodiment 13 is the method of any of embodiments 1 to 12, wherein the monoethylene glycol is in a mixture that contains less than 10 ppm aldehyde.
• Embodiment 14 is the method of any of embodiments 1 to 13, wherein the method is a continuous process.
• Embodiment 15 is the method of any of embodiments 1 to 14, wherein the contacting step is carried out at a temperature of 0 to 65 °C.
• Embodiment 16 is the method of any of embodiments 1 to 15, wherein the monoethylene glycol is fiber grade monoethylene glycol.

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• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

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• 2021
  • 2021-03-04 EP EP21714948.3A patent/EP4126357A1/de active Pending
  • 2021-03-04 WO PCT/IB2021/051837 patent/WO2021198806A1/en not_active Ceased
  • 2021-03-04 US US17/914,677 patent/US11708315B2/en active Active
  • 2021-03-04 CN CN202180025663.7A patent/CN115427146B/zh active Active
• 2022
  • 2022-09-28 SA SA522440702A patent/SA522440702B1/ar unknown

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